Вход

вход по аккаунту

Патент USA US3100706

код для вставки на сайт или в блог

Ширина: (aвто)

Высота:

ссылки на документ

адрес страницы документа

адрес полноэкранного варианта

короткий адрес

Aug. 13, 1963
l.. w. HUNTINGTON
` 3,100,701
CONTINUOUS PROCESS MINERAL SEPARATION
Filed Aug. ll,V 1960
2 Sheets-Sheet 1
Aug. 13, 1963
3,100,701
L. w. HUNTINGTON
CONTINUOUS PROCESS MINERAL SEPARATION
Filed Aug. l1. 1960
_ 2 Sheets-Sheet 2
.whUiNmM
w w.
-L,
‘I
Arroz/Eens;
United States Patent O " c1C@
Patented` Aug. 13, 1963
2
1
3,100,701
Laurance W. Huntington, Groveport, Ohio, assigner to
CONTINUOUS PRÜCESS MINERAL SEPARATION
Reno Engineering & Mining Co., a corporation of
Nevada
3,100,701
`
Filed Aufr. 11, 1960, Ser. No. 48,872
3 Claims. (Cl. 75-101)
selection are well known in the
After roasting or
drying by a conventional roperation, the material is con
veyed to a dry storage area to await its introduction into
the novel and improved separation process. It is in this
process that this invention lies.
It is well known in the art that an acid soluble metal
in certain ore [forms can be separated .from material con
taining thlat lore by maintaining the material in an acid
solution. The îtime required to separate the metal de
This invention relates to separating metal from metal
lic ore bearing material, and more particularly to a con 10 pends upon various factors including the type of ore,
`grade of ore, pH of the acid solution, the lacid used, the
tinuous process for separating acid soluble metals from
temperature, and ‘other factors which are known in the
metallic ore [bearing material at a variable controlled pH.
art. When these factors have been determined land/or
Continuous processing, in this tarea, as in others, results
selected, la person skilled in the art can compute, or esti
in substantial cost reduction over batch process methods.
mate with »a high degree ot accuracy, 4the time required
Because ofthe very low cost of this process, it is econom
to separate a predetermined amount of a given metal
ically feasible to separate acid soluble metals from metal
from the material at a given hydrogen ion concentration.
lic ore bearing material to 1obtain high grade gangme ir
With prior ant methods, a given yamount of metallic ore
respective of the commercial value of the metals removed.
bearing material is placed in a vessel, «an acid solution
If the concentration «of the metal present is such-that it
having enough hydrogen ions available `to react with a
can Ibe economically recovered, then it becomes a com
preselected desired amount fof metallic »ore is introduced;
merical lay-product; but, »the concentration of the metal
yand the reaction is allowed to continue until the' desired
does not determine the commercial feasibility of the op
percent of any given metal has been leached from the
eration; Basic-ally, 'and primarily, this process is to sepa
ore. rDhen, the mixture is filtered to separate the metal
rate ibase material from metal contained as a metallic
bearing solution and the rgangue. As used her-ein leach
ore,` whether the economic material recovered is pri
ing refers toa batch process and metal `separation is used
marily the >gangue or the metal.
Therefore, Vone of the principal objects of this invention
to refer to the continuous process.
,
The prior tart methods necessitate the use of a strongly
is to provide a substantially continuons process of sepa
acid solution. This new and novel method of separa
rating metal from metallic `ore bearing material.
A more particular object of this invention is to provide 30 tion fobviates the need of a highly acid solution through
out the process, as well as providing a substantially con
a process for separating metal from metallic ore bearing
tinuous. process.
material wherein the material is substantially continu
Referring now Ito FIGURE 2, in this new and novel
ously introduced into the process.
.process a series of reactors 10a, 10b, and 10c are pro
A more specific object of this invention is to provide
a process wherein metallic ore bearing material is sub 35 vided, the structure of which will be described presently.
FIGURE 2 sliows three reactors, but it is understood that
stantially continuously fed into one reactor, to begin
more can be connected in a similar manner. Separation
metallic separation at a controllable pH condition, and
is begun in yone reactor and continued in one or more
is therealiter‘ periodically conducted to :a second similar
reactors until completed. The separation is carried out
` reactor for continuing the separation at controllable pH
40 by forming a mixture «of metallic ore bearing material and
conditions.
water, `and bubbling sulfur oxide gas through. the mix
Another principal object of this invention is.` to pro
ture. The 4rate yof llow of the gas -is controlled in each
vide a series lof reactors for successively separating metal
reactor to provide any desired pH condition in each re
from metallic lore bearing material, and controlling the
actor.
pl-I in each reactor by introducing sulfur oxide gas at a
Thus, »at different stage-s during the process, the separa
selectable controlled rate into each reactor.
tion may be accomplished «under different pH conditions.
Another more particular object of this invention is to
Normally, most of the separation can be accomplished
provide a series lof reactors for successively separating
by controlling the rate of flow Vofthe gas, such «that- vir
metal from metallic ore bearing material at controlled
tually »as rapidly as the gas forms an acid with the water,
selectable p-H conditions with the pH in «at least one re
fthe »acid reacts with the ore. This will produce virtually
actor ‘at slightly less Ithan 7, and the pH in each reactor
a neutral condition only slightly acidic with the pH very
being controlled by introducing sulfur oxide gas at a con
‘
l close to 7. However, there may be certain metal ores in
Other objects and a fuller understanding ot the inven- 4 l the 'material' which will Vnot' react, ‘or react extremely
trolled rate.
tion may be had by referring to the following descrip
tion and claims taken in conjunction with the accom
panying drawings in which:
slowly in a slightly «acid solution, but will respond readily
to a stronger Iacid solution. Or, for some other reason,
the `operator may desire a stronger acid solution. 'This
can be 'accomplished by controlling the rate of ilow of
the suliîur oxide gas in each of the reactors t-o produce
the desired pH condition, without the necessity of main
ing material; and
i FIGURE 2. is 1a 'somewhat schematic side elevational 60 taining a strongly »acid condition throughout the process.
Ln keeping the'solution almost neutral, with the acid
View of three reactors connected in series partially in
section with parts broken away and removed.
reacting virtually as rapidly as it is formed, corrosion and
Referirng now to the drawings, and particularly 'FIG
similar
Any separation
wear onIby
theia reactors
highly acid
is reduced
solutionto
can
a be carried
URE 1, the now sheet of the entire operation is shown to
introduce environmental background for this new and
out in but a few of the reactors rather than in a single
novel process of continuons `metal separation.
“batch” reactor. `
"Material containing metallic lore is mined and trans
Further, much versatility is -added to the process by
FIGURE ’l is a flow sheet of Ithe entire operation of
` handling, preparation and treatment tof metallic ore bear
ported to a conventional crusher. Here the material is
providing optimum conditions for reaction for several
reduced to- a pre-selected size. After crushing, the mate
70 different metals in a given material. This permits a much
n'al is either roasted for dried, depending upon the type
:greater range of possible treatments in ‘a single continuous
of material and metallic ore it contains; the standards for
process.
3,100,701
3
d;
The operator, using the factors mentioned above, de
However, the pH meter and valve assemblies 21 can con
termines the pH condition to be used to separate each
trol and vary the pH in each reactor independently, by
metal and calculates vthe totaltime that an acid formed
by bubbling sulfur oxide gas through water ata controlled
regulating the ‘ate of flow of the sulfur oxide gas into each
reactor lil, the advantage `of which has been indicated.
An iii-process material outlet 23a is formed near the
bottom of the tank lia, and an in-process material inlet
24a is provided at the top of the tank lia. The material
is continuously recirculated in the reactor ltla by means
of Ia circulating’pump 22a drawing the material from the
outlet 23a `and pumping it through an -in-process material
rate must act to ‘separate the desired percentage of all the
metalsl from a metallic ore bearing material. Based on
this calculation, the number of reactors for optimum elh
ciency is selected by the operator. In all cases, at least
two reactors will be required. Normally, more than two
will be required. The total time required is then divided
by the number of reactors selected, yand the quotient rep
resents the time that the material will be retained in each
reactor. Let T represent the total separation time and
conduit 25a into the inlet 24a.
‘ The pumping action of the circulating pump 22a is aug
mented by Ian impeller agitator 16a disposed near the
t represent the time the material must remain in each
bottom of the chamber 12a; the imp-eller 16a is connected
reactor. (The time the material remains in each reactor 15 to »a drive motor i851 by a drive shaft 17a, and is formed
must be the same, the reason for which will be more fully
to induce a generally downward flow of the mixture,
explained presently.)
thus tending to force the mixture through .the outlet 23a.
AThe process is carried out at follows: The metallic ore
The agitator also performs the function mixing to main
bearing material is continuously fed into the first reactor
tain a homogeneous mixture.
with water, and sulfur oxide gas is bubbled through the 20
The in-process material also is bañled after it enters
vmixture `at a controlled rate to maintain the selected pH
inlet 24a and descends to the l`bottom of the tankV 11a.
conditi-on. After time t has elapsed, the material in the
Since all -of the sulfur oxide gas does not react to form
ñrst reactor is conveyed to the second reactor, and sulfur
acid, some escapes from the mixture and rises in the
oxide' gas is bubbled through the mixture at a controlled
reactor. As it rises, it comes in contact with the descend
rate to maintain the selected pH condition. After the 25 ing material and `further acts to form acid for metal sepa
material has remained in the second reactor for time t,
' ration 'as the material descends. From the reactor, the
if two reactors are all that Iwere selected then 2t equals T,
gases pass through a central exhaust lgas scrubber 38 to
the atmosphere.
.
Y
Y
'
and the separation has been completed and the material
is removed from the second reactor. If more than two
A sight glass 29a is provided on the tanky 11a to indicate
reactors were lselected then the material is conveyed from 30 the'level of the mixture in the tank. Using the sight glass
the second to the third reactor, where it remains for a
time t, etc., until the total time in lall the reactors equals T.
The construction and operation of each reactor is as
follows, wherein when necessary the different reactors and
their like parts are designated by a letter designation after 35
the num-ber.
~
as a guide, minor adjustments of the rate of feed into the
first reactor lita can be made to insure that preciselythe
prescribed amount of material is being charged.
A heater Sia is provided. This allows the operator to
select and control the temperature independently in each
reactor.
,
Each reactor lo has Ia cylindrical tank 11 defining an
internal chamber l2. A feed material entrance 14 is
After time t has elapsed, the material'that has been
charged into the first reactor lila is transferred to the
provided at the top of the tanky 11.k Several oppositely
-second reactor lûb. A transfer pump 32a pumps the mix
slanting, vertically staggered baffles 13 are carried by the 40 ture from the first reactor 16a out of the transfer outlet
tank 11, and are positioned in the chamber l2.v Metallic
34a through a transfer conduit 26a to the second re
ore bearing material is continuously introduced through
actor ltìb.
‘
the feed material entrance Ma into the first reactor 10a.
TheV mixture enter-s the sec-ond reactor ltl‘b through the
VThe rate of feed of the material is adjusted such that a
feed material inlet 231). Normally, Ithis mixture from
preselected amount will have been introduced into the 45 the first reactor ma constitutesv the entire charge of the
first reactor 10a in time t. This amount is a function of
second reactor 1Gb. The metal separationis continued
the capacity of reactor 16a. The material is baffled Vin its
in the second reactor by the introduction of sulfur oxide
downward descent through the chamber 12 and eventually
drops to the bottom of the reactor.
Y
- gas in the same manner aas in the first reactor.
The rate
of flow of the gas is controlled by the pH meter valve
Water is introduced into the first reactor 10a through 50 assembly 2lb; again, the pH is normally maintained at
a Iwater entrance 15a and iiows to the bottom of the re
actor. Thus, a mixture of material and water collects at
the bottom of the first reactor 10a.
Sulfur .oxide gas is introduced into this mixture through
gas pipes 20a projecting into this mixture. The gas pipes
20a project to different depths in the mixture to promote
a more uniform Vdistribution of thev gas as it enters the
mixture, Iand thus la more uniform pH throughout the `
less, slightly, than~7if possi-ble. Also, the mixture is
agitated `and recirculated in the same manner as in the
first reactor.
-
When time t has elapsed, the mixture is pumped out
of the second reactor lltib. If the separation is not com
pleted, the material is pumped from the second reactor
ltlb to the third reactor itl'c and the separation continued
similarly as` in the second reactor 10b, `and so on into
mixture. The gas -pipes 29a in turn are supplied by a gas
ladditional reactors if necessary until the separation has
conduit 19u. The sulfur oxide gas is supplied from a
been completed.
‘
central producer 36 which is connected to the gas supply 60
The transfer operation is controlled by a time sequence i
conduit 19 by a gas supply main 37.
’
A pH meter and valve assembly 21a is provided to
regulate and control the ñow of sulfur oxide gas. The pH
meter and valve assembly 21a can be adjusted to allow
control mechanism 412 associated with solenoid operated
gate valves 4l disposed in the transfer conduits 26. After
the prescribed amount of time z has elapsed, each of the
gate valves 41a, dfb, Iand ¿lic is opened by the time
`a fiow of gas to produce and maintain a preselected pH 65 sequence control 42, ‘and the transfer pumps simultane
of the mixture. Normally the pH selected will be slightly
less .than 7, where possible `as described above. The flow,
yas thus selected, ywill constantly be producing a rather
ously transfer the material from each reactor to the next
successive reactor land remove the material from the last
reactor. Hence, the first reactor 10a is exhausted of the
small amount of hydrogen ions; and, virtually as rapidly 70 material collected during the time t. As the material
as the hydrogen ions are being produced, they are reacting
is pumped from the second reactor 10b to the third re
with the metallic ore. Thus, ‘an almost neutral condition
can be maintained, and «still a reaction can be carried on.
actor 10c, the material is being pumped from the first
reactor llíla to the second reactor ïílb, etc. The feed of the'
Effectively, a controlled limited amount of hydrogen ions
material continues in the first reactor lita, and, after the
`are continuously being made available for the reaction. 75 next period of time t, the proper amount of material will
3,100,701
5
have collected in the first reactor and the transfer opera
tion is again performed. Thus, a continuous process
ensues, with the material constantly being fed into the first
reactor 10a, and the resultant product periodically being
moved successively to each reactor and removed from the
6
to Without departing from the spirit and the scope of the
invention hereinafter claimed.
What is claimed is:
f
'1. 'In a continuous process of separating metals from
a metal-bearing material by progressively treating the
last reactor.
material in a series of reactor vessels under different pH
Each transfer conduit 26 has a ball check valve, not
shown. Such valve will prevent any reverse flow of
material.
conditions, the steps of continuously introducing water
and material into the top portion of the first vessel in the
series, flowing the mixture of water and material along a
tortuous path toward the bottom of the first vessel, in
When the separation has been completed, the mixture
is transported to a conventional filter; and the solution
containing the separated metal is filtered off the gangue.
If the recovery of the metal in solution is economically
feasible, it is precipitated out, filtered, and funther con
ventionally processed. The separated gangue, remaining
after the filtering, is roasted thus readying it for economic
commercial sale. The resultant product is a gangue, free
of kdeleterious metal and ready for sale.
The liquid remaining after the precipitated metal is
filtered off is principally water with some acid. This can
be used as the water introduced into the process, until
troducing a gaseous reagent into the bottom of the first
vessel and producing -a counter-current flow of reagent to
the top of the Vessel, continuously circulating the mixture
and the reagent in the bottom portion of the first vessel,
'recirculating the reagent treated mixture by pumping it
from the bottom to the top of the first vessel, continuously
pumping the recirculated mixture from the bottom of the
first vessel to the top of the second vessel, and repeating
in subsequent vessels the steps performed in the first
vessel.
2. The process as claimed in claim l wherein the
gaseous reagent is introduced into the first vessel by an
the acidity reaches a predetermined amount, after which
initially directed flow toward the bottom wall of the ves
it is discarded.
sel, and wherein the mixture of Water and material and
This process has been found to be highly successful
for separating metallic compounds from sodium salts of 25 the reagent is circulated in the bottom portion of the ves
sel by mechanical agitation which tends to force the
sea Water, and to render the Water salt-free and potable.
mixture against the bottom Wall of the vessel and up
Raw sea water is introduced into the first reactor 10a,
wardly along its side Walls.
and reacted progressively through the series of chambers
3. A continuous process of treating material contain
as above-described. After leaving the last of the reac
tors, the water is filtered to remove dirt and other undis 30 ing metallic components with sulphur dioxide gas pre
paratory to subsequent further treatment, comprising the
solved debris and then treated with lime to convert the
steps of, providing a plurality of deep reaction chambers
sulfur compounds of the various metals other than so
having agitation means therein supplying a flowable form
dium into their insoluble oxide forms. The product is
of material to be treated to one said chamber, applying
then filtered to remove the precipitated metallic oxides.
The sodium chloride remains in solution free of contami 35 sulphur dioxide gas into said one chamber below the
surface of the material to be treated and causing an agi
nating metals. The water is then evaporated to leave
tation of said material as the gas is supplied, monitoring
substantially pure sodium chloride free of other contami
said contents to determine the pH value at all times and
nating metals and the evaporated water is condensed as
altering the rate of sulphur dioxide flow to maintain a
a potable water suitable for irrigation and other water
uses.
40 controlled pH condition selected to dissolve Apart of the
metallic components in said material, transferring some
Therefore, this process is useful for separating sea
of the material from the said one chamber to the next
Water into saleable metallic oxides, sodium chloride free
chamber and continuously replacing the amount removed
of contaminating metals, and useful water.
with fresh source material, recirculating the material
In summary, it is believed that the invention resides
in providing a process into which metallic ore bearing 45 from the bottom to the top of the chamber as well as
agitating and circulating the material at the bottom of
material is continuously introduced into a first reactor
the chamber, ‘and treating the material transferred with
where the rock is partially separated at a selected con
gas in like manner to the treatment in the prior chamber
trolled pH condition, land thereafter conveyed to one or
while monitoring to prevent an acidic condition.
more similar reactors, one at a time, where the separation
process is‘completed, at selectable controlled pH condi 50
tions.
Although the invention has been described in its pre
ferred form with a certain degree of particularity, it is
understood that the present disclosure of the preferred
form has been made only by Way of example and that 55
References Cited in the ñle of this patent
UNITED STATES PATENTS
1,245,137
Vad-ner ______________ _.. Oct. 30, 1917
1,266,731
Westby ____________ __ May 21, 1918
540,366
Canada ____________ __ Apr. 30, 1957
FOREIGN PATENTS
numerous changes in the details of construction and the
combination and arrangement of parts may be resorted